Heat exchanger for high prandtl number fluids

ABSTRACT

A fluid heat exchanger including a channel for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein a length of at least one segment being set in relation to a hydraulic diameter and a Prandtl number of the first fluid, and a first pattern flow disruptor interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel.

BACKGROUND Technological Field

The present disclosure relates to a heat exchanger, and more particularly to a heat exchanger for a high Prandtl number fluid.

Description of Related Art

A variety of devices are known in the heat exchanger area. However High-Viscosity/Prandtl-number fluids such as oils or glycol solutions result in poor heat transfer and high pressure drop. Surface augmentations are often used to enhance heat transfer; however, result in even higher pressure drop.

The conventional methods and systems have generally been considered satisfactory for their intended purpose. However, there is still a need in the art for heat exchanger having improved heat transfer capabilities. There also remains a need in the art for such heat exchangers and components that are economically viable. The present disclosure may provide a solution for at least one of these remaining challenges.

SUMMARY OF THE INVENTION

A fluid heat exchanger includes a channel for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein at least one segment of the at least two segments defines a length greater than five times a hydraulic diameter of the channel, and a first pattern flow disruptor interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel, and a second series of channels for passing a second fluid therethrough for transferring energy to the first fluid. A first segment of the at least two segments can define a length different from a length of a second segment of the at least two segments. The length of the first segment can be defined by the equation 5D_(h)<L<4D_(h)Pr wherein L is the length of the first segment, D_(h) is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment. The length of the second segment can be defined by the equation 5D_(h)<L<4D_(h)Pr wherein L is the length of the second segment, D_(h) is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment.

The segments of the first flow pattern can be aligned in the same direction. The segments of the first flow pattern can be straight. The first pattern flow disruptor can narrow the flow channel. The first pattern flow disruptor can change a direction of flow of the first fluid. The first pattern flow disruptor can include multiple disruptors, wherein at least one of the flow disruptors includes a longer length than another disruptor.

A method of transferring heat between fluids includes directing a fluid through a heat exchanger channel and developing a thermal boundary layer between the fluid and a surface of the channel and a momentum boundary layer between the fluid and the surface of the channel, wherein the thermal boundary layer of the fluid includes a different thickness than a thickness of the momentum boundary layer, and directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid.

The fluid includes a Pradntl number greater than 1, or preferably a Prandtl number greater than 7. The thermal boundary layer of the fluid is thinner than the momentum boundary layer. A ratio of thermal boundary thickness to momentum boundary layer thickness can decrease along a flow direction of the fluid and the ratio of thermal boundary thickness to momentum boundary layer thickness can be greater than 1.

These and other features of the systems and methods of the subject disclosure will become more readily apparent to those skilled in the art from the following detailed description of the preferred embodiments taken in conjunction with the drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

So that those skilled in the art to which the subject invention appertains will readily understand how to make and use the devices and methods of the subject invention without undue experimentation, preferred embodiments thereof will be described in detail herein below with reference to certain figures, wherein:

FIG. 1 is a perspective view of a heat exchanger;

FIG. 2 is a perspective view of a heat exchanger plane of FIG. 1, showing a channel for transporting a fluid;

FIG. 3 is a perspective view of an alternate embodiment of FIG. 1, showing a second type of flow disruptor; and

FIG. 4 is a perspective view of an alternate embodiment of FIG. 1, showing a third type of flow disruptor.

DETAILED DESCRIPTION

Reference will now be made to the drawings wherein like reference numerals identify similar structural features or aspects of the subject invention. For purposes of explanation and illustration, and not limitation, a partial view of an exemplary embodiment of a heat exchanger channel in accordance with the invention is shown in FIG. 1 and is designated generally by reference character 100. Other embodiments of heat exchanger channel in accordance with the invention, or aspects thereof, are provided in FIGS. 2-4, as will be described. The methods and systems of the invention can be used to improve heat transfer using fluids with a high Prandtl number.

Referring to FIG. 1, a heat exchanger 100 having multiple channels for passing fluids therethough is shown. The heat exchanger 100 includes a hot fluid inlet 102, a cold fluid inlet 104, and a header 106. The disclosure focuses on the structure of the individual channels for the hot fluid and the cold fluid.

Referring to FIGS. 2-4, a channel 108 for passing a first fluid therethrough is arranged along a primary axis 110 including at least two segments 112, 114 of a first flow pattern. A first segment 112 defines a length L1 that may be different from a length L2 of a second segment 114, and a first pattern flow disruptor 116 is interspersed between each of the segments of the first flow pattern to enhance heat transfer of the fluid flow along the channel 108. The channel 108 can include multiple segments of the first flow pattern, and multiple disruptors 116. The length of the first segment L1 is defined by the equation 5D_(h)<L1<4D_(h)Pr wherein L1 is the length of the first segment, D_(h) is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment 112, and the length of the second segment is defined by the equation 5D_(h)<L2<4D_(h)Pr wherein L2 is the length of the second segment, D_(h) is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment 114. The Prandtl number can be calculated at the midpoint of each segment. However, an average Prandtl number can be used, as the number is not expected to vary substantially within each segment. The Prandtl number is a dimensionless number defined as the ratio of momentum diffusivity to thermal diffusivity. Wherein the momentum diffusion rate is dependent of the dynamic viscosity and density of the fluid along a heat exchange channel, and the thermal diffusivity is dependent of the thermal conductivity and density of the fluid, which again varies along the flow path. Using an expected steady state Prandtl number of fluid flowing through a heat exchanger, the heat exchanger channel is sized accordingly.

The segments 112, 114 of the first flow pattern are aligned in the same direction. The segments 112, 114 of the first flow pattern can be straight. As shown in FIG. 2, the flow disruptor 116 can be a sinusoidal path attached to the straight first flow pattern. As shown in FIG. 3, the flow disruptor 116 can be straight flow and set-off from the first flow pattern. As shown in FIG. 4, the first pattern flow disruptor 116 can narrow the flow channel or change a direction of flow of the first fluid. It is further contemplated that the first pattern flow disruptor 116 can include multiple disruptors between each of the first flow pattern portions 112, 114. The disruptors can be of various shapes and sizes. The disruptors can include various lengths along the same path, which can be beneficial for channels for larger changes in Pr.

A method of transferring heat between fluids using a heat exchanger is also disclosed. The method includes directing a first fluid through a heat exchanger channel and developing a thermal boundary layer between the first fluid and a surface of the channel and a momentum boundary layer between the first fluid and the surface of the channel, wherein the thermal boundary layer of the first fluid includes a different thickness than a thickness of the momentum boundary layer. Directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid. The first fluid includes a Pradntl number greater than 1, or more specifically a Prandtl number greater than 7.

For fluids with a Prandtl number above 1, the thermal boundary layer of the first fluid is thinner than the momentum boundary layer. A ratio of thermal boundary thickness to momentum boundary layer thickness decreases along with the flow of the fluid and the ratio is always greater than 1.

The method described above is leveraged to augment heat transfer while reducing pressure drop penalty by intermittently disturbing the flow at desired intervals, where the momentum profile is allowed to recover while the thermal profile remains augmented. For fluids having a high Prandtl number the flow through the first segment (L1) result in lower pressure drop with little degradation to the enhancement in heat transfer caused by the disruptor. The optimal length the disruptors can be selected based on expected steady state conditions and fluid properties. The implementation of this method has shown an improvement of approximately 30% more heat transfer with respect to conventional methods, while keeping the pressure drop penalty unchanged.

The methods and systems of the present disclosure, as described above and shown in the drawings, provide for a heat exchanger with superior properties heat transfer. While the apparatus and methods of the subject disclosure have been showing and described with reference to embodiments, those skilled in the art will readily appreciate that changes and/or modifications may be made thereto without departing from the spirit and score of the subject disclosure. 

What is claimed is:
 1. A fluid heat exchanger comprising: a channel for passing a first fluid therethrough arranged along a primary axis including at least two segments of a first flow pattern, wherein a length of at least one segment being set in relation to a hydraulic diameter and a Prandtl number of the first fluid; and a first pattern flow disruptor interspersed between each of the segments of the first flow pattern configured to reduce a pressure loss of the fluid flow along the channel.
 2. The heat exchanger of claim 1, wherein at least one segment of the at least two segments defines a length greater than five times a hydraulic diameter of the channel.
 3. The heat exchanger of claim 1, wherein a first segment of the at least two segments defines a length different from a length of a second segment of the at least two segments.
 4. The heat exchanger of claim 3, wherein the length of the first segment is defined by the equation 5D_(h)<L<4D_(h)Pr wherein L is the length of the first segment, D_(h) is the hydraulic diameter of the first segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the first segment.
 5. The heat exchanger of claim 3, wherein the length of the second segment is defined by the equation 5D_(h)<L<4D_(h)Pr wherein L is the length of the second segment, D_(h) is the hydraulic diameter of the second segment, and Pr is the expected steady state Prandtl number of the first fluid at a location along the second segment.
 6. The heat exchanger of claim 1, wherein the segments of the first flow pattern are aligned in the same direction.
 7. The heat exchanger of claim 1, wherein the segments of the first flow pattern are straight.
 8. The heat exchanger of claim 1, wherein the first pattern flow disruptor narrows the flow channel.
 9. The heat exchanger of claim 1, wherein the first pattern flow disruptor changes a direction of flow of the first fluid.
 10. The heat exchanger of claim 1, wherein the first pattern flow disruptor includes multiple disruptors.
 11. The heat exchanger of claim 10, wherein at least one of the flow disruptors includes a longer length than another disruptor.
 12. The heat exchanger of claim 1, further comprising a second series of channels for passing a second fluid therethrough for transferring energy to the first fluid.
 13. A method of transferring heat between fluids comprising: directing a fluid through a heat exchanger channel; and developing a thermal boundary layer between the fluid and a surface of the channel and a momentum boundary layer between the fluid and the surface of the channel, wherein the thermal boundary layer of the fluid includes a different thickness than a thickness of the momentum boundary layer.
 14. The method of claim 13, wherein the fluid includes a Pradntl number greater than
 1. 15. The method of claim 13, wherein the fluid includes a Prandtl number greater than
 7. 16. The method of claim 13, wherein the thermal boundary layer of the fluid is thinner than the momentum boundary layer.
 17. The method of claim 13, wherein a ratio of thermal boundary thickness to momentum boundary layer thickness decreases along a flow direction of the fluid.
 18. The method of claim 17, wherein the ratio of thermal boundary thickness to momentum boundary layer thickness is greater than
 1. 19. The method of claim 13, further comprising directing a second fluid through a second channel adjacent to the first channel and transferring heat from the first fluid to the second fluid. 